Batch control using bang-bang control

ABSTRACT

A method for batch control in a system. The system comprises at least two batch processing sets that share at least one shared equipment. A batch is initiated in each processing set. Process variables from each batch are monitored. At least one process variable from at least one batch are adjusted using bang-bang control to prevent conflicts.

CROSS REFERENCE TO RELATED APPLICATION

This application is a continuation-in-part of co-pending U.S. patent application Ser. No. 12/773,485, filed May 4, 2010, the technical disclosure of which is hereby incorporated by reference in its entirety.

BACKGROUND

1. Technical Field

The present invention relates to a method for advanced control of batch processes.

2. Description of Related Art

Many types of products are made in batch or semi-batch processes. Often the control systems for batch processes are relatively crude compared to continuous processes. One reason for this is that it is often difficult to measure the product in a batch process. Moreover, the quality characteristics of the final product are only directly evident at batch completion. Further, as one skilled in the art would understand, often batch processes also exhibit large time constants and time varying gains and dynamics. As such, complex nonlinear dynamic models are needed for control models, which are often unavailable for industrial processes. Because it is often difficult to measure the properties of a product until the end of the batch, the basic automation system generally attempts to repeatably adhere to defined recipe conditions in the hope that these conditions will yield acceptable product. For future batches if the actual value was different than the expected value, then the recipe of the process conditions of the future batch can be adjusted. Thus, prior art batch process control systems are feedback or reactionary control systems. Such basic control systems cannot or do not proactively compensate for the incoming disturbances that are inherent in any process. As such, basic control systems in batch operations often have great variability in the final product specifications compared to continuous processes that can be continuously monitored and adjusted to meet a desired final specification. Accordingly, it is desirable to have an advanced batch control system that can offer better control over the batch system by decreasing variability. Further, it is desirable that an advanced batch control system be able to better predict and obtain desired final product properties, as well as improve process efficiency and process operability.

BRIEF DESCRIPTION OF THE DRAWINGS

The novel features believed characteristic of the invention are set forth in the appended claims. The invention itself, however, as well as a preferred mode of use, further objectives and advantages thereof, will be best understood by reference to the following detailed description of illustrative embodiments when read in conjunction with the accompanying drawings, wherein:

FIG. 1 a illustrates the overall control architecture in one embodiment.

FIG. 1 b illustrates the control architecture at a decision point in one embodiment.

FIG. 1 c illustrates the feedback architecture in one embodiment.

FIG. 2 illustrates the connectivity of the advanced control system in one embodiment.

FIG. 3 is a flow diagram for one embodiment.

FIG. 4 is a flow chart illustrating the system development in one embodiment.

FIG. 5 illustrates a side-profile view of a kettle in one embodiment.

FIG. 6 is a graphic depiction of one batch topography showing temperature trajectories against time.

FIG. 7 illustrates the gas flow rate profile of a kettle fryer in one embodiment.

FIG. 8 is a side profile view of a shared slicer and conveyor in one embodiment.

FIG. 9 is a temperature and gas flow rate profile for two batches in one embodiment.

FIG. 10 is a graph showing the concentration of Acrylamide as a function of batch size in one embodiment.

DETAILED DESCRIPTION

Several embodiments of Applicants' invention will now be described with reference to the drawings. Unless otherwise noted, like elements will be identified by identical numbers throughout all figures.

In one embodiment a method for advanced batch control over a batch process is disclosed. In one embodiment the advanced batch controller comprises optimization problems that are solved to provide actionable targets, such as set points, for controllers at the Programmable Logic Controller (hereinafter “PLC”) level or the Distributed Control System (hereinafter “DCS”) level. In one embodiment optimization problems are posed in a way that ensures that pre-selected targets for key process variables or final product quality variables are met and result in changes to the PLC set points that are needed to reach the target values.

As will be discussed in more detail below, the method can be applied to batch, semi-batch, and transient portions of continuous processes. Generally, batch processes are processes where all the materials are charged into a vessel at the start of the batch and then processed for a finite time under time varying process conditions. Thereafter, at some condition that defines the end point, such as a passing of a fixed amount of processing time or the achievement of a certain condition, the final product is discharged from the batch process. As used herein a “material” refers to any material placed into a batch process. As used herein a “final product” refers to the product as it exists when the batch process has finished or when the product is removed from the batch process. Semi-batch processes are like batch processes except that some material is charged or discharged during the transient portions of the batch.

Additionally, continuous processes often comprise transient portions such as during start-up, during shut-down, or during transition from a first operating condition to a second operating condition and can occur during product grade changes, for example. Such transitional processes are transient because there is a definable start time and a finish time. In one embodiment, the advanced batch controller can be applied to control and refine these transient portions of continuous processes. As such, the term batch, as used herein, shall refer to batch, semi-batch, and transient portions of continuous processes.

In one embodiment the advanced batch control methodology is based upon the following: (i) developing empirical or semi-empirical models of the transient operation based on data collected from batches under existing operation and under conditions in which designed experiments have been performed; (ii) defining a finite number of decision points throughout the progress of the batch process at which control will be applied; (iii) using the models for each decision point and the available measurements at those points to predict the final product quality attributes or the features of the transient operation that it is desired to control; (iv) developing advanced control algorithms for use at each decision point based on the use of the models and their predictions at each decision point and on measurements that will be available at each decision point; (v) implementing these control algorithms in real time on new batches at each decision point using the models and controllers developed for those decision points and the measurements from the new batch that are available at each decision point.

Data Collection

The first step in the advanced batch control method is the collection of data. The data are used to build a model which can be employed by the control algorithm. In one embodiment, a model refers to a mathematical description of the batch process. As discussed above, the models may be empirical, semi-empirical, or fundamental models. As used herein a control algorithm refers to any algorithm, analytical or numerical optimization solver that calculates or estimates a control action. The advanced batch controller comprises the combination of a model and a control algorithm.

The data can be acquired with many methods and devices known in the art. In one embodiment the data are acquired using one or more of the following protocols: Object Linking and Embedding for Process Control Data Access (OPC-DA), Object Linking and Embedding for Process Control Historical Data Access (OPC-HDA), Open Database Connectivity (ODBC), or vendor specific data acquisition protocols such as those defined by the data historian vendor, OSI-PI. Those skilled in the art will understand how to collect and store the data.

The data are collected on at least one batch cycle but in one embodiment is collected on multiple cycles. A cycle begins with the initiation of the batch and finishes upon the completion of a batch. The amount of data to be collected and the number of batch cycles included in the collected data will depend on the specific embodiment being monitored. In one embodiment, collecting data on a single batch results in an acceptable model. As will be described herein in some embodiments the model includes a corrective bias whereby the model can adjust overtime to become more accurate by comparing the predicted result with the actual result. In other embodiments the data are collected on two or more batches to obtain a more complete data set to build a more accurate initial model. In one embodiment a model is progressively adjusted to yield better results batch after batch. In one embodiment better results comprises decreased variability. In one embodiment, more than two batches are monitored to provide a data set. Further, in one embodiment the batch conditions during data collection are similar to the conditions in which the model will be utilized.

In one embodiment the advanced batch controller can be configured to run a batch or series of batches according to a programmed design so that the batches can be suitably perturbed and the data recorded. This allows for the collection of high quality data for building or updating the model over a variety of conditions.

As will be discussed in more detail below, empirical, semi-empirical, and fundamental models may be employed to create the advanced batch control or algorithm. In one embodiment, the model is based, at least in part, on empirical results. In some embodiments strictly fundamental models are unfavorable as it is costly and time consuming to build reliable fundamental models for a real industrial process. Furthermore, often some aspects of the process may be very difficult, if not impossible, to model. Fundamental models can often only use variables that can be explicitly accounted for in the mechanisms described by these models. Contrariwise, empirical or semi-empirical models can extract and incorporate useful information from all available measurements; even obscure measurements that may not be incorporated into a fundamental model, such as torque on an agitator shaft, for example, may be accounted for in the empirical models. Consequently, most embodiments utilize only empirical or semi-empirical methods as opposed to strictly fundamental methods. Semi-empirical methods are understood to mean a hybrid modeling method in which models of fundamental mechanisms are combined with empirical modeling methods. In one embodiment the semi-empirical methods include a hybrid of fundamental mechanisms combined with empirical modeling methods that account for those phenomena not captured by the fundamental part of the model. One example would be to incorporate dimensionless numbers, such as the Reynolds Number, as additional variables in an otherwise purely empirical model. Another example would be to compute some fundamentally meaningful quantities such as the energy released due to reaction from some direct measurements, such as temperatures and flows. These calculated fundamental variables are then used as variables in building the semi-empirical models.

In one embodiment, the collected data comprises data relating to at least one process variable. In other embodiments the collected data comprises a plurality of process variables. A process variable is anything that can either affect or is indicative of the processing of a batch. There are many types of process variables, including the measurable properties of the material as well as process conditions. A measurable property of the material includes any measurable property of the material. This includes, but is not limited to, molecular weight, moisture content, percent solids, viscosity, density, texture, color, etc. A process condition is any measurable processing condition of the batch. This includes, but is not limited to pressure, temperature, time, the rate of heating or cooling, the rate of a fluid being supplied to a jacket, gas or liquid flow rate, duty of a burner or heat exchanger, the speed of an agitator, the torque of an agitator, the rate of a circulating pump, etc.

The collected data also include data associated with the final or intermediate product properties. A “final product property” refers to any measurable property of the final product. An “intermediate product” is a product that has been processed in the batch but is not yet a final product. The final or intermediate product properties can include, but are not limited to moisture content, salt content, oil content, percent solids, color, texture, level of a compositional compound including but not limited to Acrylamide, percent purity or impurity, conversion, temperature, density, viscosity, molecular weight, concentration, coating thickness, etc. Essentially, anything that can be measured on the product in a quality control lab that is important to the end use of the product can be considered a product property. In one embodiment the final or intermediate product properties are measured by on-line instruments located at the end of the batch. In other embodiments the final or intermediate product properties are measured off-line, for example in a quality control laboratory. In one embodiment the final or intermediate product properties are measured days or even weeks after the completion of the batch. In such an embodiment, the model is built using past data where these measurements have been made and the advanced batch controller then controls the predicted values of these to a set point with minimum variability about that set-point.

The data collected can include time histories of one or more process variables referred to as process variable trajectories. For example, if the temperature of a batch is monitored over time, the resulting temperature trajectory, including slope, minimum and maximum points, average temperatures, etc. can also be collected. Likewise, data related to discrete trigger events may also be collected. This would include, as an example, an agitator or pump turning on or off at a certain time in the process or in response to a reached processing condition.

Model Creation

After collecting data on at least one process variable then at least one model is created. Further, an advanced batch controller is created which uses the model to generate outputs.

As discussed, a wide variety of data can be included in the models. In one embodiment the data are directly relatable to a final product property. For example, in one embodiment the temperature of a batch can have a direct effect on the final product properties. In other embodiments a relationship exists with interpreted data. Interpreted data can comprise many forms. In one embodiment calculations of the data results in a relationship with a final product property. For example, the interpreted data may comprise determining the slope of the data over a given time. In such an embodiment, the slope of the data may have a relationship on a final product property. Other interpreted data can include initial values, final values, maximum and minimum values, average values, variances, etc. Thus, in one embodiment while creating the model, the data is interpreted to see which features of the interpreted data have any impact on the process variables being modeled. Both the data and the altered data can be included in the created model.

There are a variety of methods to create the model including, but not limited to, partial least squares, canonical correlation regression, reduced rank regression, multi-linear regression including higher order polynomial terms, nonlinear regression, ridge regression, neural networks, fundamental mechanisms such as dimensionless groups, mass and energy balances, differential equation sets or a combination thereof. A good discussion of model building and solving can be found in, “Control of batch product quality by trajectory manipulation using latent variable models”, Flores-Cerrillo, J. and J. F. MacGregor, J. Process Control, 14, 539-553, 2004, the entirety of which is incorporated herein by reference.

In one embodiment the models are exported electronically from offline model building software and repackaged for online use without manual intervention. In one embodiment the models comprise parameters that are updated recursively in real-time.

In some embodiments, when modeling a batch process it is useful to include the time histories of key measured process variables. The process history of a process variable can have a high degree of autocorrelation. Accordingly, the value at one point in time often exhibits a strong correlation with values at earlier points in time. This can cause the data to be ill-conditioned numerically. As a result, for some embodiments, latent variable regression and related methods such as ridge regression can provide stable empirical models for this type of data.

In one embodiment, the advanced batch controller is formulated as a generic quadratic programming problem. In one embodiment the problem is convex, can be solved efficiently, and can accommodate any relevant constraints to be imposed on the variables. An example of the quadratic programming problem is given below. In one embodiment, the quadratic programming problem formulation may be described by the following, or equivalent, equation set:

min_(MV) I=(CV _(PRED) +CV _(BIAS) −CV _(SP))^(T) W ₁(CV _(PRED) +CV _(BIAS) −CV _(SB))+α₁ SPE+α ₂ T ²+α₁(MV−MV _(SB))^(T) W ₂(MV−MV _(SP))  (1a)

Subject to:

SPE≦UCL _(SPE)  (1b)

T ² ≦UCL _(T) ₂   (1c)

LB _(MV) ≦MV≦UB _(MV)  (1d)

[CV _(PRED) ,SPEX,T ² ]=PLS(MV,DV)  (1e)

W ₁ =dtag(w ₁)  (1f)

W ₂ =dtag(c ₁)  (1g)

The objective function is defined in equation (1a). The constraints to be obeyed are shown in equations (1b) to (1d). The model, in this case formed with Partial Least Squares (PLS) is shown equation (1e). The model can also be formulated explicitly as a set of constraints. The definition of the diagonal weighting matrices is shown in equations (1f) and (1g). The terms in equation (1) are defined in Table 1 below.

TABLE 1 Definition of Terms Term Definition MV Vector of manipulated variables - In one embodiment these are the set points that will be written to the PLC. CV Vector of controlled variables - In one embodiment these are the process conditions and final product properties that are to be controlled. SPE Squared prediction error - a measure of deviation from the correlation structure defined by a latent variable model T² Hotelling's T² - a measure of extrapolation within the latent variable model plane) Subscript PRED Predicted value Subscript BIAS Feedback bias adjustment Subscript SP Set point (target value) W_(i) Quadratic penalty matrices α_(i) Penalty weighting factors

It should be noted that the terms, α₁SPE+α₂T^(e), in the objective function relate specifically to the use of a PLS model. These terms penalize extrapolation from the validity space of the PLS model. If a different model type were to be used, these terms can be replaced by a different metric or set of metrics for model extrapolation, as suitable to the chosen model type or types. The same is true of equations (1b) and (1c), which specify upper bounds on these two metrics. These constraint equations would be replaced with suitable constraint equations for the extrapolation metric(s) for the chosen model type or types. Further, regarding equation (1e), the equation indicates the specific choice of a PLS model type. However, any other model type or types, as relevant to the problem, or to the preference of the practitioner, could be used, the notation in equation (1e) being updated accordingly.

The models can comprise one, or a plurality, of inputs and outputs. An input is anything entered into the model and/or the advanced batch controller. In one embodiment a model comprises model inputs and model outputs. A model input is anything inputted into the model. In one embodiment, model outputs comprise controlled variables and/or predicted variables. In one embodiment, model inputs comprise manipulated variables and/or disturbance variables. As used herein “control output” refers to any result produced by the advanced batch controller. If a model output is produced by the advanced batch controller, then the model output is also a control output. As an example, if the model produces a predicted variable, that predicted variable can be considered a control output and a model output. Further, if the model input is produced by the advanced batch controller then that model input is a control output. In one embodiment the control output comprises instruction or data sent to the process by the advanced batch controller. In one embodiment the control output comprises only a single output whereas in other embodiments the output comprises a plurality of outputs. A process condition set point refers to the set point of a process condition. The control output can include, but is not limited to instructions to adjust process variables, including manipulated variables, a process condition set point, a predicted process variable, or a predicted final product property. As an example, one control output may comprise a set point of 240° F. Thereafter, the process is adjusted in order to reach the specified set point temperature. As used herein reaching a set point or condition refers to obtaining the set point within the acceptable tolerance. If the acceptable tolerance is +/−5% of the set point, then coming within that tolerance range is considered reaching the set point. In one embodiment the tolerance range is from 0 to about 20%, whereas in another embodiment the tolerance range is from 0 to about 10%. In still another embodiment the tolerance range is from 0 to about 5% and whereas in another embodiment the tolerance range is from 0 to about 1%.

Additionally, the control output may include a predicted intermediate product property. As noted above, it is often difficult, if not impossible, to accurately measure some product properties while being processed in a batch. As such, the model can predict the product properties at various points during processing. The model can predict intermediate product properties and final product properties. In some embodiments an intermediate product property must be reached before the next step of processing is applied. One example refers to chemical reactions and the corresponding conversion. A process can require that a specified amount of conversion take place before further processing. Consequently, the model may be used to predict the intermediate product property at some point during the batch process. The intermediate product properties can include the final product properties previously described. In one embodiment, the control output comprises a product property set point or instructions to reach the product property set point. A product property set point is a desired product property that the advanced batch controller attempts to reach.

As stated earlier, virtually any measurable process variable can be inputted into the models. The inputs can be specified as being either manipulated variables (MV's) that can be implemented or disturbance variables (DV's) that can only be observed. Examples of manipulated variables include those process variables which can be manipulated by the advanced batch controller. These include, but are not limited to, the process conditions listed above. Disturbance variables are those process variables which the control system cannot or does not control. Examples of disturbance variables include the product properties of the materials fed into the batch process. These can include the percentage of solids of a material entering the batch, the moisture content of the material, the initial temperature of the material, the molecular weight, etc. The disturbance variables can also include process conditions that affect the batch but that cannot easily be controlled. For example, atmospheric pressure at a given altitude, ambient temperature and ambient humidity are disturbance variables that can be taken into account but often are not easily compensated for. As an example, a model created for a process at sea level can be modified to a process at 6,000 feet of altitude by accounting for these disturbance variables. Taking the disturbance variables into account allows the model to account for non-uniform conditions even if these non-uniform conditions cannot be controlled. Another example includes the weight or composition of materials charged to the batch which can be variable, their moisture content, or the amount of impurities in the materials.

FIG. 1 a illustrates the overall control architecture in one embodiment. In one embodiment, the PLC collects and transmits data concerning the process. This data is transmitted to the relevant platform. As previously stated, in one embodiment this platform can collect data from a variety of locations including for example, a historical database. The data is then transmitted to the advanced batch controller, shown here as D1 and D2. The advanced batch controller receives parameters from the configuration structures. These configuration structures are described below herein in reference to FIG. 3. These configuration structures can include control configuration structures, model parameter structures, and data parameter structures. These configuration structures provide the parameters to be used by the control algorithm and the model.

The relationship between the control algorithm and the model is shown in FIG. 1 b which is an enlarged subset of FIG. 1 a. FIG. 1 b illustrates the control architecture at a decision point in one embodiment. The model submits a manipulated variable to the control algorithm as shown by the SOLVER and the control algorithm submits a manipulated variable to the model. Thus, the manipulated variable is an input into the model but an output from the control algorithm. In one embodiment this process is completed iteratively until the manipulated variable is optimized. In one embodiment the manipulated variable comprises a vector of a plurality of optimized manipulated variables. The advanced batch controller then sends the optimal manipulated variable, the control output, back to the platform. The platform transmits this to the PLC which controls the process.

In one embodiment the input variables can be constrained by lower and upper bounds. Further, the variables can be constrained by inequality and equality constraints. One such example would be a valve position. A valve can only be 100% open or 0% open, or somewhere in between. Accordingly, a constraint can be placed on a valve position indicating that the number must be a positive real number ranging from 0 to 100. Further, in one embodiment these constraints can be updated dynamically as needed. In one embodiment the advanced batch controller comprises multiple constraints. In one embodiment the advanced batch controller comprises a combinatorial inequality constraint. An example of a combinatorial inequality constraint is when a weighted summation of two or more variables must be below an upper limit or above a lower limit. For example, if the sum of the masses of two or more materials added to the batch must be below an upper limit. In one embodiment the advanced batch controller comprises an equality constraint. In such an embodiment, two or more flow rates, or added amounts of materials, must be maintained in a fixed ratio. For example, for every pound of material A added to the batch process, two pounds of material B must be added.

In one embodiment one or more constraints, as described above, can be updated dynamically, either within a batch or from one batch to the next. For example, if a particular phase of a batch must be completed by a certain time, then a constraint on the maximum duration of that phase can be adjusted dynamically based on the sum of the durations of the preceding phases, which could vary from batch to batch.

In one embodiment some input variables are more relevant that other input variables. Accordingly, in one embodiment the manipulated variables are ranked in relative importance by applying relative weights in the manipulated variable penalty term. In one embodiment, these weights are forced to sum to one, but in other embodiment they are not. In addition, in one embodiment the manipulated variables are in scaled rather than their original engineering units. These considerations help maintain a consistent magnitude for this term regardless of the number of manipulated variables or choice of engineering units, thus aiding controller tuning. Further, this helps ensure that the optimization problem is numerically well conditioned. Those skilled in the art will understand that determining whether to rank the variables and assigning relative weights will be dependent on the specific embodiments. Further, in one embodiment a bias and/or multiplying factor can be applied to the calculated value for each manipulated variable before sending the instructions to the process. This provides additional tuning handles if needed.

In one embodiment, the model also includes a term that allows target values to be set for the manipulated variables. This can be used to specify ideal resting values for certain manipulated variables if there are excess degrees of freedom in the control problem. In addition, it allows relative costs to be applied to the manipulated variables so that secondary economic objectives can be built into the optimal control problem. For example, in one embodiment there are two sources of energy input to the batch process, such as a steam heat exchanger and an electric heating element. One heating source may have a more immediate effect on the process than the other. Conversely, one heating source may be considerably more expensive than the other per unit of energy delivered to the batch process. Having two sources of heating typically implies an excess degree of freedom. If economics are a primary driving force then an ideal resting value of “low” or “off” can be used for the expensive heating source. The advanced batch control system can then only manipulate this input away from its ideal resting value if the other heating source is at its maximum heating value and still more heat is required. Conversely, if fast dynamic response is a primary objective then an ideal resting value can be specified for the heating source that has a slower impact on the process, so that the advanced batch controller preferentially manipulates the heating source that has a rapid effect on the process. Thus, in one embodiment, the optimization formulation is run to co-ordinate the objectives of the one or more decision points so as to optimize one or more objectives including, but not limited to economic, operability, and performance objectives. In one embodiment the objectives consider cost of materials, operating costs, as well as any economic benefit such as selling price of the final product. In one embodiment the relative weight of the objectives is specified via a weighting matrix.

In one embodiment, model outputs can be specified as either controlled variables (CV's) that are to be controlled, or predicted variables (PV's) that are merely to be predicted. In one embodiment the controlled variables includes a desired process condition. For example, the controlled variable can include a temperature set point. Altering the temperature set point alters the temperature trajectory, for example. Additionally, the controlled variables can include instructions for reaching a desired process variable or process condition. For example, if one controlled variable is the desired temperature, the advanced batch controller can instruct a valve to open the flow of heating fluid to increase the batch temperature. In one embodiment the advanced batch control communicates with the PLC control layer. Further, a control variable may include instructions for the batch to hold for a period of time.

In another embodiment the controlled variables include final product quality attributes. For example, the controlled variable can be the moisture content of the final product once it is removed from the batch process. In such an embodiment, the advanced batch controller can manipulate one or more process conditions, including the duration of the batch as one example, so as to reach the target moisture content at the end of the batch.

Predicted variables can include predicted process variables or predicted intermediate or final product quality attributes. By definition, the model merely predicts this variable or variables for use outside of the control system, but does not take any control action itself with respect to these predicted variables.

Time is another process variable which can be predicted and controlled. As an example, it is often desirable that a batch finish at a desired point in time, referred to as a desired finish time. The actual time at which the batch is finished is referred to as a finish time. One common example is where two batches are combined into a single batch for further processing. In such an example, it is often desirable that both batches finish at approximately the same finish time. Thus, the advanced batch controller, utilizing the model, can receive data regarding two or more batches and adjust one or both of the batches so that a specified processing step occurs at about the same time in both batches or that the batches finish at about the same finish time. Likewise, an advanced batch controller can adjust the processing of a batch so that the batch is completed in the specified time such as to conform to standard practice. Accordingly, in one embodiment the advanced batch controller receives input from other batches and utilizes that information in its control. In another embodiment, the objective is to complete the batch process in the shortest time possible so that the average rate at which product is produced is maximized. This is desirable since it produces economic benefits.

Since batches may not all run for the same total period of time, either overall or within a specified phase of the batch, some embodiments require that time over the entire batch or within a batch phase be warped so that all batches can be compared and modeled on a consistent basis. In such an embodiment, the evolution of the batch is warped against an indicator variable, which can be time itself, or another variable that may be more suited to describing the degree to which the batch has evolved. One example is conversion. The batch may be said to be complete when a certain percentage of one or more key materials have been converted, via reaction, to the finished product. In such an embodiment, the evolution of the batch can be warped so that the process variables are sampled at consistent increments in percent conversion, rather than consistent increments in time itself. In another embodiment, dynamic time warping methods, such as those developed originally to aid speech recognition, can be used to warp the measured process variables. Other related methods for warping the batch trajectory variables may also be used.

In one embodiment, controlled variables and manipulated variables can be given a specific target, with deviations penalized quadratically, or a by using a deadband range. In the latter case, the predicted variable value is penalized quadratically only when outside the deadband range. In one embodiment the model takes into account desired manipulated variable set points and the disturbance variables to formulate the desired objective.

In one embodiment, as discussed above in reference to the manipulated variables, the controlled variables are assigned relative weights that can be forced to sum to one. In other embodiments the relative weights are not forced to sum to one. As stated previously, those skilled in the art will be able to determine the relevant weights to assign to the different controlled variables. In addition, the controlled variables can be in scaled rather than their original engineering units. These considerations help maintain a consistent magnitude for this term regardless of the number of controlled variables or choice of engineering units, thus aiding controller tuning.

In one embodiment, the model further comprises a feedback mechanism. Feedback from measurements of the control output variables from previous batches is provided via a feedback bias term for at least one or more controlled variables. Thus, information on the actual measured product quality or process conditions reached in a batch are compared to the values of those predicted by the model. Corresponding feedback corrective action can then be applied to the model predictions for subsequent batches. The feedback corrective action can be calculated in a variety of methods including using an exponentially weighted moving average of the error. Another method includes using a process disturbance model.

FIG. 1 c illustrates the feedback architecture in one embodiment. As depicted, the feedback mechanism receives data. The data can be received from the PLC controller or from other means such as data sent from an off-site quality control laboratory. The feedback updater and the model will then determine new optimal parameters which can be utilized by the advanced batch controller.

In one embodiment, the controlled variable bias is updated automatically by an appropriate choice of filtering on the error between the predicted and measured values. This feedback mechanism can integrate out sustained offsets between predicted and measured values. These offsets can be due to a variety of circumstances including measurement drift whereby a sensor or other measurement equipment begins to drift over time. A feedback mechanism accounts for and overcomes such offsets. Thus, in one embodiment, the feedback mechanism allows the model predictions to remain accurate over time.

In one embodiment the parameters of the model itself are updated recursively with time in response to the feedback described above. Thus, in one embodiment the model itself is made to track changes in the process, therefore maintaining accurate model predictions over time.

In one embodiment, a partial least squares model is used to describe the batch process and adherence to this model is enforced via penalty terms on Squared Prediction Error (SPE) and Hotelling's T². Those skilled in the art will understand that these and other such methods can be used to determine if the extrapolation exceeds the space of the model. Other such monitoring tools and methods can be utilized to monitor the error of the model. The Partial Least Squared model can include snapshot inputs, trajectory variables and/or customized features extracted from the trajectory variables. Similarly, in one embodiment, the control outputs can comprise a snapshot measurement and/or trajectory variables, such as particle size distribution for example. In one embodiment, the SPE and Hotelling's T² terms are normalized, for example by their respective 95% confidence limits. Alternatively, other embodiments the confidence limits are greater than about 95%, whereas in other embodiments the confidence limits are about 99%. Virtually any confidence limit can be used. This helps maintain a consistent magnitude, which aids controller tuning.

In one embodiment, the SPE, Hotelling's T² and manipulated variable penalty terms each have an overall penalty weight. This allows the relative importance of all terms in the optimal control objective function to be weighted appropriately.

In one embodiment the control output is checked against one or more criteria including, but not limited to, SPE, Hotelling's T², individual score values, and/or optimization convergence criteria in order to determine whether or not to control the control calculations. In one embodiment, explicit constraints are applied to SPE and Hotelling's T² in the quadratic programming formulation, as seen in equation (1). Alternatively, in another embodiment, these statistical variables are not explicitly constrained during the optimization problem. Instead, the values of SPE and Hotelling's T² corresponding to the optimal solution are compared to the acceptable limits. If either is above such limits the control action is not implemented.

In one embodiment, once a model has been created, and the specific controller formulation specified in the control algorithm, the batch process is initiated. The optimal control is calculated at a key decision point during batch evolution. A decision point is a point in time where the created model and specified controller formulation is applied to obtain an objective. At the decision point the advanced batch controller, utilizing the model, can predict and/or control either the batch processing conditions or the product properties or both. The decision point or points can be located at various times throughout the batch. The location of a decision point can be time dependent or dependent upon the happening of a triggering event. Thus, a decision point may be located a time of 2 minutes into the batch processing or the decision point may be located when the batch reaches a specified temperature, pressure, percentage conversion, addition of a key material, initiation of a specific processing step such as heating, agitation, etc.

In one embodiment the results of the model calculations at a given decision point are written synchronously to one or more data sinks. One embodiment utilizes a generic data platform for this purpose. Likewise, in one embodiment the data is acquired synchronously at a given decision point from one or more data sources, such as at the plant, in real-time. For example, if one of the inputs is material initial temperature, the data related to that input can be received from a thermocouple and introduced into the model to perform the calculations at the decision point. If the desired data is missing or not yet available, missing data imputation methods can be used at a given decision point. Missing data imputation allows the predictions and control to be performed using only the available measurements with minimal impact due to the missing measurements. Missing data imputation methods for latent variable models include but are not limited to, single component projection (SCP), projection to the model plane (PMP), conditional mean replacement (CMR), trimmed score regression (TSR) expectation maximization (EM) and optimization based approaches for imputing the missing values as known by those skilled in the art.

In other embodiments the model can specify the input instead of receiving the actual input from a data source. As an example, in one embodiment a first decision point specifies the mass of a particular material to be added to the batch. A second decision point thereafter can later use the measured actual mass added, if it is available. If it is not available it can be estimated using missing data methods as described above.

In one embodiment data reconciliation is applied for all inputs and control outputs to screen for gross errors in the measured inputs or outputs. Measurements that are deemed unreliable are set to missing and are reconstructed using the data correlation structure captured by the corresponding model, via a missing data method, as described above. For example, if a measured input is routinely 300° F. and the measured temperature is 4,000° F., then that measurement can be deemed missing and replaced by methods described above.

Some processes may only require a single decision point. Other embodiments comprise one to two decision points. Other embodiments comprise one to three decision points, whereas other embodiments comprise one to four or more decision points. In other embodiments ten or more decision points are utilized.

Multiple decision points are possible and each can have its own unique model and/or own unique control objectives. Put differently, in some embodiments a separate model is created and utilized for each decision point. In other embodiments a single model is used for each decision point. In still another embodiment a single model is used for a plurality of decision points, and separate models are used for one or more of the other decision points. Those skilled in the art will be able to determine if a separate model is required for each decision point, or whether two or more decision points can use the same model. Likewise, in some embodiments separate control algorithms are created and utilized at each decision point whereas in other embodiments the same control algorithm is used for each decision point.

In one embodiment, at the decision point the selected inputs are inserted into the model. The model's outputs together with the specified control algorithm are used to control and operate the batch until the next decision point or until the end of the batch. As an example, the model at the decision point may determine that to reach the specified final product property the temperature of the batch must be increased and held for a period of time. The advanced batch controller can then increase the temperature as specified by the optimal solution on the model and hold it for the suggested period of time. Thereafter, a second decision point can then offer additional process control instructions or the batch would finish. The second decision point can occur after the hold time suggested by the first decision point or it may occur before the suggested hold time has expired.

In one embodiment the decision points have separate objectives. In one embodiment the objectives are dissimilar. For example, one decision point may have an objective of calculating and obtaining the next process condition set point. The process condition set point can be a desired temperature, pressure, etc. As an example, at a decision point the advanced batch controller takes the inputs and calculates the next desired temperature set point. The advanced batch controller at that decision point then instructs the PLC or equivalent control layer how to proceed in order to reach the new desired temperature set point. Put differently, this decision point determines the set point of a desired process variable trajectory. The advanced batch controller then adjusts the system as necessary to obtain the desired process variable trajectory. In the case of a temperature trajectory, the advanced batch controller adjusts the system to mimic the desired temperature trajectory.

Thereafter, in one embodiment a second decision point has a dissimilar objective of reaching a final product property or an intermediate product property. As noted, a second decision point can take place any time after a first decision point. The second decision point can take place a specified time following the first decision point, or it can occur after an initiating event such as a set point being reached or the happening of an event such as an agitator initiating. In the example above wherein the advanced batch controller at a first decision point calculates a desired temperature set point, the second decision point can take place at, prior to, or subsequent to the reaching of that calculated desired set point. Thus, in one embodiment the first decision point has an objective of reaching a desired temperature, whereas a second decision point has an objective of obtaining a final product moisture content. The model at the second decision point predicts the final product moisture content, compares the predicted with the desired moisture content, and the advanced batch controller adjusts process variables as necessary. Virtually any final product property which has any correlated effect with a process variable can be controlled. In one embodiment a batch process comprises a plurality of decision points at which time the model predicts the final product property or properties.

Further, in one embodiment multiple final or intermediate product properties are sought simultaneously. In such a case each final or intermediate product property can be assigned a relative weight so that the model knows which property is the primary consideration.

In still other embodiments two or more decision points may have similar objectives. Continuing the example from above, one embodiment comprises a decision point wherein the advanced batch controller calculates a temperature set point and controls to mimic the desired temperature trajectory. Thereafter at a second decision point the advanced batch controller recalculates the temperature set point so that the desired temperature trajectory can be reached. Three, four, and/or five decision points each calculating process conditions then follow. Finally, a sixth and final decision point calculates process variables so that a final product property is reached.

One skilled in the art can appreciate that decision points having dissimilar objectives can be intermixed. Carrying the previous example, a first decision point calculates a temperature set point and controls the batch to mimic the desired temperature trajectory. Subsequently, a second decision point calculates the predicted final product property and determines if it is within acceptable tolerances of the desired final product property. If the advanced batch controller determines that the desired product property will not be reached it can readjust the process by adjusting one or more process variables. Thereafter, a third decision point recalculates the temperature set point and controls the batch as necessary to mimic the desired temperature trajectory. Subsequently, a fourth decision point determines if any action is necessary to obtain the desired final product property. The process can be repeated as necessary.

In one embodiment, at a given decision point, the advanced batch controller always calculates and implements a control action. Conversely, in another embodiment the advanced batch controller predicts what the intermediate or final product quality will be if the nominal processing conditions are adhered to. If it is predicted that the intermediate or final product quality will fall within an acceptable tolerance region, the advanced batch controller does not calculate and implement any control action. Put differently, in such an embodiment the advanced batch controller allows the nominal processing conditions to be adhered to.

Implementation

Once an advanced batch controller is in place the resulting data can be tracked. In one embodiment the history and product information for each batch is packaged into a generic data structure and stored electronically. In other embodiments a summary of the history and product information from each batch is collated and stored electronically in a log file.

Once created the advanced batch controller can reside in any location that allows it to be coupled to the plant control layer such as the PLC or DCS. Thus, the advanced batch controller can reside on a computer that is a node on the plant control Local Area Network (LAN), in communication with a plant control server, etc. The advanced batch controller can be located on site or can be stored remotely and operate via the interne or wireless network. Those skilled in the art will understand the various ways to couple the advanced batch controller with the existing control system.

In one embodiment, the advanced batch controller acts in a supervisory manner on top of the existing PLC/DCS based control layer. In some embodiments the system acts like an autopilot which can instruct and override the existing PLC/DCS based control layer as necessary. In one embodiment the advanced batch controller is accessed, configured and monitored through the design of a user interface for graphical display of calculated multivariate data. In another embodiment the controller is accessed, configured and monitored through the design of a user interface for manual entry and manipulation of targets, bounds and various tuning parameters that affect controller execution.

FIG. 2 illustrates the connectivity of the advanced batch control system in one embodiment. In the embodiment depicted the process to be monitored and controlled is connected to an Object Linking and Embedding for Process control (OPC) server. The OPC server is coupled to an operator's computer which oversees and monitors the process. In one embodiment the operator has an override which allows he or she to control the system directly. Also coupled to the OPC server is the advanced batch control server. As discussed, this server can be located on site or be located remotely. Further, in one embodiment a single server acts as both the OPC and the advanced batch control server. Coupled to the advanced batch control server is a database. The database pulls and archives data received from the process. The data can be received from either server or the operator's computer. The database may be located on a separate server, or may be integrated into either the OPC or the advanced batch control servers. Those skilled in the art will understand that in some embodiments a single server or computer can serve all purposes described.

Also coupled to the database is a system design and model building tool. In one embodiment this tool comprises a computer having optimization software. The system design and model building tool can be connected at all time so that the model is constantly updated and adjusted. Further, the tool may adjust the model at regular times, either automatically or via manual intervention. In one embodiment, a model building and refining exercise is performed by process personnel using suitable software. In other embodiments after the model is created then the model building tool is not connected to the system. While model building is described, those skilled in the art will understand that the tool can also be used for re-building of the models.

In one embodiment, also coupled to the database are one or more computers. I one embodiment, these computers are remote. These computers allow the process to be monitored and/or controlled in real time. An example would be a computer for a plant manager that can oversee the processes of several processes remotely. In one embodiment, these remote computers can only receive data. Thus, they can view the process but otherwise exert no control over the process. In other embodiments, however, the remote computers can exert control over the system. Further, in one embodiment the remote computers can update targets, bounds and various tuning parameters that affect controller execution in real-time. In one embodiment there is a real-time view on the batch evolution and the advanced batch control implementation is provided via a view client that can run in a web browser. Such an embodiment allows seamless access from any computer that can connect to the network to which the computer running the advanced batch controller is connected.

In one embodiment, the advanced batch control server receives data. The data is then transmitted to the necessary unit which runs the model on the received data. The control output variables are then relayed to the OPC server which implements its instructions to the process. At the next decision point the model will incorporate the necessary inputs and relay a second set of control output variables. The process is repeated until the batch is completed. In one embodiment data from completed batches is stored so that the model can be adjusted as needed. Accordingly, in one embodiment the model is being adjusted with the completion of each batch. In another embodiment the model is adjusted, if needed, after a specified number of batches have been completed.

FIG. 3 is a flow diagram for one embodiment. The diagram demonstrates, among other things, the logic utilized to determine if control action is required in one embodiment. At the decision point the model can predict, for example, a final product quality. If the predicted property is within the acceptable tolerance of the desired property then no action may be needed. This decision is then passed to the data manager and then down to the PLC control layer. If the predicted property is not within the acceptable tolerance of the desired property then action is necessary. The advanced batch controller then makes the necessary adjustments to system. The diagram also shows where data parameters, such as constraints or necessary product conditions can be inputted into the platform. Further, the figure illustrates an embodiment wherein the advanced batch controller calculations are modularized by use of encapsulated structures for the data object as shown by the DATA PARAMS, the model object as shown by the MODEL PARAMS, and the controller configuration object shown by the CONTROL CONFIG. In one embodiment the model, control algorithm, and the data are handled via encapsulated structures in software to streamline the code and provide a packaged record of all conditions related to the execution of each batch cycle. In one embodiment the model object comprises the math model, for example as determined by Partial Least Squares. In one embodiment the controller configuration comprises the parameters that define the objective function and constraint set of, for example, the equation defined in equation (1a) above. In one embodiment, the data object comprises an electronic record of the data received from both the batch, and the advanced batch controller. Having a modularized structure has several benefits. First, it allows the code to be modular which results in streamlined code. Second, it allows for the packaging of recorded data. After a number of batches are completed the results, predictions, parameters, etc. can be summarized and stored for later retrieval and utilization. For example, the data from multiple batch cycles can be retrieved in a suitably packed form and used to update the model parameters for online use. This activity is demonstrated by the label “System Design and Model Building” in FIG. 2. The data can also be used to provide summaries of the performance of the advanced batch controller, which can be used to report to management, decide when to schedule maintenance on the models and/or control algorithms, etc. An additional benefit in one embodiment is that the models can be built and maintained so that the models are current and reflect process operation faithfully. In one embodiment the models can be rebuilt in a separate software package. In one embodiment the rebuilding software package is ProMultiVariate made by ProSensus, Inc., of Hamilton, Ontario, Canada. In one embodiment the modular encapsulation allows the users to better summarize each batch. Additionally, in one embodiment the modular encapsulation allows easier integration with analytical tools such as Matlab. Accordingly, in one embodiment the modular encapsulation standardizes the data structure.

FIG. 4 is a flow chart illustrating the system development in one embodiment. The chart begins with designing experiments which will allow the user to collect the relevant data. Such an experiment can be used to determine any rough correlations between process variables and final product properties. Thereafter a feedback method is designed, if desired, and the viewers are designed.

The advanced batch controller results in increased control over the batch and decreased product variance. Because, in one embodiment, the advanced batch controller is a feed forward control system as opposed to a feedback control system, the controller can more consistently achieve the desired product properties. In one embodiment, final product property variability decreases by about 50% compared to the variability without the advanced batch controller. In another embodiment, final product property variability decreased by more than 50% compared to the variability without the advanced batch controller.

Kettle Batch Example

One embodiment utilizing advanced batch control of a batch kettle fryer will now be described. This description is for illustrative purposes only as the method can be utilized in a variety of embodiments.

As the name implies, batch process kettle frying of potato chips involves placing a batch of potato slices in a kettle of hot oil, e.g., at a temperature of about 300° F. (about 150° C.). In the conventional kettle fryers used in the production of kettle-style chips, the cooking oil temperature follows a generally U-shaped time vs. temperature profile as illustrated in FIG. 5 of U.S. Pat. No. 5,643,626, assigned to the same assignee as the present invention, the entire disclosure of which is hereby incorporated by reference. Upon introduction of the potato slices into the oil, the temperature of the oil typically drops quite rapidly by as much as 50° F. (about 28° C.) or more. This drop in temperature is partially due to the introduction of a large mass of comparatively cooler potatoes. As depicted by FIG. 5, the oil temperature falls to a low point temperature of about 240° F. (116° C.) for a low point time of about 4 minutes. After measuring the low point temperature, heat to the kettle is then quickly increased and then the temperature of the oil begins to gradually rise, reaching about the initial frying temperature of about 300° F. (roughly 149-150° C.). The resultant potato chip'has a moisture content of between about 1.5% to about 1.8% by weight.

The modern kettles that are utilized in batch processes are generally manufactured of stainless steel, and vary in size and capacity. FIG. 5 illustrates a side-profile view of a kettle in one embodiment. As depicted the kettle 508 is heated by gas burners positioned directly under the kettle floor and supplied gas from a gas supply. In one embodiment, fryer capacities range from 100 to about 220 pounds of potatoes per batch. In another embodiment, the fryer comprises 140 to about 220 pounds of potatoes per batch. In another embodiment, the fryer comprises about 150 to about 170 pounds of potatoes per batch. In order to efficiently use a batch kettle fryer of a given size, it is necessary to maintain a particular “load” or amount of potato slices per volume of oil, in order to achieve the desired frying temperatures. These and other constraints provide limits on the amount of throughput using batch kettle fryers.

As depicted, the kettle 508 further comprises a stirrer 507. The stirrer 507 moves throughout the kettle 508 to stir the potato slices 509. In one embodiment, the stirrer 507 comprises two temperature probes: a stationary temperature probe 501 and a mobile temperature probe 502. The temperature probes can comprise any probe known in the art. In one embodiment, the stationary probe 501 is located toward the bottom of the kettle 508, though various locations are suitable. The mobile probe 502, in one embodiment, is located at about the same depth as the stationary probe 501.

In the prior art operation, once the batch was complete then the stirrer 507 was directed upstream whereby it subsequently pushed the potatoes out of the kettle 508 via the discharge conveyor 506. However, often there was a lag in time of about 30-40 or more seconds whereby the potatoes were ready to be discharged but the stirrer 507 was not in position. Thus, the batch could not discharge the potato slices until the stirrer 507 was positioned upstream near the entrance conveyor 505. This contributes to some product being fried for longer than the desired time, often increasing product variability. In an attempt to overcome these deficiencies, the stirrer 507 was positioned at the upstream end once a pre-discharge temperature had been reached. This approach, however, was insufficient to reduce variability.

There are several differences between the advanced batch controller as applied to the kettle fryer and the prior art control system. Previously, as discussed above, the high burner was instructed to initiate only after a minimum temperature was reached. The timeliness of this instruction was often delayed due to instrumentation lag. Thus, the prior art utilized a feedback control system which resulted in increased variability of final product properties such as moisture content. The advanced batch controller, however, utilizes a feed forward control. This allows the advanced batch controller to predict the time to switch to high gas flow rather than simply reacting to the temperature of the batch as monitored by a thermocouple which could introduce unwanted instrumentation lag. As will be seen below, application of the advanced batch control method results in more consistent final product properties, specifically moisture content.

Further, the advanced batch controller allows the pre-discharge temperature to be dynamically calculated based, in part, upon the location of the stirrer 507. For example, if the stirrer 507 is at the downstream end of the kettle 508, the pre-discharge temperature will be lower than if the stirrer 507 is near the discharge position located in the upstream end. In one embodiment, utilizing a dynamic pre-discharge temperature calculation reduced the standard deviation of the discharge temperature by over 50%. This reduction in variation improved the ability to make accurate predictions regarding final product moisture. In one embodiment the calculation is performed at the PLC layer.

Further, batch weight was often previously used as a tool to manipulate the processing time. In one embodiment, changes in batch weight results in increased product variability. In one embodiment, applying advanced batch control allows the processing time and other such variables to be achieved while keeping the batch weight constant. This results in decreased variability.

A series of kettle chip batch process cycles were first monitored and the resulting data collected. The monitored operation was similar to the embodiment depicted in FIG. 4. A BF360 Batch Fryer from Heat and Control, Inc. of Hayward, Calif. was used as the kettle.

To obtain models which capture fundamental relationships in the process variables measured, a designed data collection procedure was established and followed. High and low values for many process variables were specified. In one embodiment, these included, the weight of potatoes fed to the fryer (“batch weight”), the solids content of said potatoes, the initial oil bath temperature at the start of the batch, the flow rate of heating gas at low fire at the start of the batch, the time to switch from low fire to high fire, the gas flow at high fire, the period of time to hold the high fire condition (“high fire duration”), the gas flow at low fire after switching from high fire, and the recovered oil temperature at which to begin discharging potato chips from the fryer. In one embodiment, a multivariate model was created using partial least squares. As noted above, however, methods other than partial least squares can also be used to develop the model.

One embodiment comprised two decision points. It was found that with some embodiments of this particular batch process two decision points offered better control and decreased variance compared to a single decision point. The variables used in the optimization problems solved at the first and second decision points were constrained with bounds to ensure that any suggested settings are reasonable and will not pose operational difficulties when applied at the PLC layer. For example, lower and upper bounds were placed on the gas flow at low or high fire conditions so that extreme deviations from the nominal values were prevented. Similarly, lower and upper bounds were specified on the mass of potatoes that the advanced batch controller could specify to be fed to the batch. In like manner, lower and upper bounds were placed on high fire duration and also on the temperature at which discharge of potato chips commences, etc. Similar to specific target values that are inputted into the advanced batch controller, these bounds can be set. The models at both decision points comprised bound settings defined in configuration files that can be modified as needed over time to ensure continued good operation of the controllers.

In one embodiment the high fire flow rate was set to range between about 2,500 to about 4,500 scfh. In such an embodiment, the max capacity on the burner was 4,500 scfh. Thus, the high fire flow rate in the algorithm was constrained to be below 4,500 scfh. In one embodiment, the low fire flow rate was set to range from about 300 to about 1,000 scfh.

In one embodiment, the lower bound on high fire duration was calculated dynamically for each batch so that the advanced batch controller could not specify a time to switch back to low fire that was earlier than the location of the second decision point. This provides a specific example of the method of modifying constraints on the control problem dynamically.

The two decision points are illustrated in FIG. 6. FIG. 6 illustrates a temperature profile of a kettle fryer in one embodiment. The bold line 601 is the temperature profile as measured by the stationary oil probe 501. The light line 602 is the temperature profile as measured by the mobile temperature probe 502. In one embodiment, the initial temperature (T₀) was inputted into the model. Further, in another embodiment, the temperature difference between the temperature as measured by the stationary 501 and the mobile 502 probes was inputted into the model. In yet another embodiment, the slope of the temperature as measured by the stationary probe prior to the initiation of the batch (T_(slope,0)) was used by the model. This provides examples of data interpretation being utilized in the model formulation.

At each decision point the model defined the settings for variables used to control the batch process via a PLC server. The first decision point (D1) took place a short time after the batch begins. As can be seen in the figure, the temperature of the oil dropped rapidly after the introduction of the potatoes.

In one embodiment, the objective of the first decision point (D1) was to ensure the process reaches a desired minimum temperature. It is generally believed that the U-shaped temperature-time profile imparts the intense flavor and unique mouth feel characteristics of kettle-style chips. Accordingly, in one embodiment of the kettle process it is desirable that a minimum temperature be reached to control the U-shaped temperature-time profile. At the first decision point the model used its list of manipulated variables (MV's) to meet the chosen target for minimum temperature. This is done by simultaneously accounting for and/or adjusting batch weight (BW), the time at which to switch to high gas flow (SW1), and the initial gas flow rate (G0). In one embodiment the batch weight was targeted to a predetermined weight unless it was needed for control purposes. In one embodiment the measured variables that are available at the first decision point include the initial batch temperature and solids concentration of the potatoes. These disturbance variables (DV's) are compensated for by the advanced batch controller by manipulating the specified batch weight, low fire gas flow and switch time (MV's) to ensure that the targeted minimum oil temperature is achieved as closely as possible. For example, the advanced batch controller comprised the ability to increase or decrease the gas flow in order to increase or decrease the kettle temperature as needed based on the control output from the first decision point.

FIG. 6 illustrates the gas flow rate profile of a kettle fryer in one embodiment. As can be seen in the figure, the gas flow rate was changed from an initial flow rate (G0) to a high gas flow rate (G1) and to an intermediate gas flow rate (G2) depending on the outputs of the model. Further, the time between an initial (G0) and a high gas flow rate (G1) was also controlled by the advanced batch controller. It should be noted that in other embodiments the model can also comprise other process variables such as agitation, pressure, etc. As such, the first decision point (D1) resulted in adjustments to ensure a desired trajectory is achieved.

In one embodiment, the second decision point (D2) comprised an objective to reach a desired final product property, specifically moisture content. In one embodiment the desired final moisture content is about 1.6%. While in one embodiment moisture content was used as a control point, in other embodiments multiple final product properties can be simultaneously used as a control point. For example, the second decision point (D2) can be utilized to obtain a desired oil content, percent solids, color, level of a compositional compound including but not limited to Acrylamide, and percent purity or impurity. Further, as previously discussed, the final product properties can be assigned relative weights which signify which property is of primary significance, which is of secondary significance, etc.

The second decision point (D2) can include the data used in the first decision point (D1) calculation as well as the first decision point variables as measured in the process as a result of applying the first decision point control action. The input disturbance variables for the second decision point included the actual batch weight, potato solids percentage, initial oil bath temperature at start of batch, slope of oil bath temperature at start of batch (T_(0,slope)), time to switch from low to high gas fire (SW₁), actual average low gas flow at start of batch (G_(0,actual)), actual average high gas flow (G_(1,actual)), trajectory of oil bath temperatures (stationary and wireless temperature probes) and the trajectory of the difference between these until the second decision point. The input manipulated variables included the duration of high gas flow period (HGD) as shown on FIG. 5, the temperature at which to start discharging the potato chips from the fryer (T_(discharge)), and the target for low gas flow at the end of the batch (G2). As noted above, the advanced batch controller can adjust a variety of process variables in order to reach the desired targets. Thus, the second decision point estimated both the discharge time and batch temperature of the batch.

The variables used in the optimization problems solved by the models at the first (D1) and second (D2) decision points were constrained with bounds to ensure that any suggested settings were reasonable. Further, they were constrained to ensure that they will not pose operational difficulties when applied at the PLC layer. For example, the maximum setting for high gas flow duration has an upper bound as previously described. Further, each of the first and second decision point advanced batch controllers bound settings are defined in configuration files that can be modified as needed over time to ensure continued good operation of the controllers.

As noted previously, the location of the stirrer 507 often prevents the potatoes from discharging at the desired time and/or temperature. To overcome this problem, the location of the stirrer 507 was inputted into the control algorithm. This allows one objective to ensure that the stirrer 507 is in the upstream location when the discharge temperature is reached. Accordingly, the discharge temperature, and the associated trajectory, can be adjusted to ensure the stirrer 507 is positioned as desired when the appropriate discharge temperature is reached. In one embodiment the discharge temperature ranged from about 290° F. to about 320° F. In another embodiment the discharge temperature ranged from about 298° F. to about 308° F. In one embodiment, values for minimum temperature in the temperature profile ranged from about 245° F. to about 260° F. In another embodiment the minimum temperature ranged was about 255° F.

The application of the advanced batch control method resulted in significantly greater control over the system. This resulted in decreased variability which can translate into increased product compliance. Table 2, below, summarizes the results of the advance batch control on a batch kettle fry potato chip system. Data were collected on about 60 batches using conventional control and about 99 batches using advanced batch control. As can be seen, product moisture variability was reduced by about 53.8%, oil variability was reduced by about 57.0%, and minimum batch temperature variability was reduced by about 52.3%. The changes in the mean values for the controlled variables were the result of slightly different choices of set point targets for these values over the values that commonly result form the pre-existing control system prior to implementing advanced batch control.

TABLE 2 Variance Reduction Summary No Parameter ABC Control With ABC Control Percent Change Moisture Mean 1.514 1.658 9.457 Std. Dev. 0.107 0.049 −53.788 Variance 0.011 0.002 −78.645 Oil Mean 28.194 31.654 12.271 Std. Dev. 2.490 1.070 −57.039 Variance 6.202 1.145 −81.544 Minimum Temp. Mean 253.639 249.237 −1.73534 Std. Dev. 3.558 1.696 −52.3227 Variance 12.658 2.877 −77.2687

As discussed above, the methodology applies to batch and semi-batch processes, and transient portions of continuous processes. One such example is the batch production of tortilla chips. Corn is typically stored and processed in kettles and cooked for a period of time until a desired hydration is obtained. Advanced batch control can be applied to this process to ensure the desired hydration is obtained by adjusting processing time, temperature, and other variables.

Advanced batch control can also be applied to vacuum frying and/or baking. In both of these processes one final product property that is controlled is final moisture content. The advanced batch control method can be used to optimize the process control, obtain the final moisture content, and reduce product variability.

Likewise, advanced batch control can be applied to liquids as well. One example is brewing of beer whereby the amount of hops, grains, water, yeast, as well as the process conditions can be optimized to increase control and reduce product variability. Another example is in the batch processing of certain dairy-based products such as cheese, casein, yoghurt, butter, ice cream, specialty dairy-based powders, dairy-based desserts, chocolate, etc.

The advanced batch control method can be applied to non-food processes as well. One such example is a batch polymerization process. In one embodiment, at a decision point at the start of the batch the advanced batch controller can adjust the amount of initiator or catalyst or the temperature of the reactor to compensate for measured material property variations, while at decision points later in the batch cycle the controller can use measurements on the temperature trajectories, the agitation power, the reactor pressure, etc. to adjust manipulated variables such as the initiator or monomer feed rates, the reactor temperature, the desired batch duration, etc. in order to achieve a desired molecular weight, viscosity, particle size, etc for the final product.

These processes can be continuous in nature, such as a polymerization process, but as discussed above, comprise portions that are transient. One specific example is the changing of a product grade in a continuous polyolefin process. During this change the process operation is moved from producing one product grade with desired melt index and density properties to another grade with different values of these properties. The advanced batch control method can be applied during this transient time in order to optimize the transition, for example by completing the transition in the shortest possible time which minimizes the amount of product that does not comply with the specifications of either grade. Alternatively, many polymer products are produced in batch reactors. One example includes emulsion polymerization reactors. In such embodiments advanced batch control can be used to implement corrective action at one or more decision points during batch evolution so as to minimize variability in final product quality, amongst other possible control objectives.

The method can also be applied in measurement analytics. In many of these analytics variances as high as or higher than 15% are acceptable. One example of such analytics includes a gas chromatograph. This machine operates as a batch process. As such, advanced batch control methods can be applied to optimize the consistency of operation of the machine.

The method also has application in many bioreactors. Examples include ethanol fermentation, biopharmaceutical production, and waste water management. Waste water management often operates as a series of batch processes with each process having a desired goal for the treated water. The applied method can optimize control over the process and decrease variability in the quality of the treated water. In bioreactors control is applied at various decision points to manipulate the feed rate of nutrients, adjust the temperature pH or dissolved oxygen level in the medium in order to achieve high yields of final product and constrain the concentrations of various byproducts in the final product to fall within acceptable limits.

The method also has application in many metal operations such as the production of steel or aluminum. Aluminum is often produced with electrolysis in a smelter. This batch process can be optimized with the advanced batch control method. Steel is produced in electric arc or basic oxygen furnaces and the final composition of Carbon, for example, can be controlled by using the advanced batch controller to manipulate the amounts of various additives charged to the vessel and energy added to the process at various decision points during the batch.

Many semiconductors are manufactured in batch processes. The advanced batch control method can be utilized in the processes of vapor deposition and etching, among others, to control and achieve the final properties of the products at the end of the batch. As one example, the thickness of the deposited or etched layer on a wafer can be controlled by manipulating gas feed rates, and the desired end time for the batch.

The method can also be applied in the manufacturing of specialty chemicals, mining operations, adhesives, inks, agricultural chemicals, emulsion polymers, paints, bulk and solution polymers, powders, mixes, and active pharmaceutical ingredients, machined parts, reaction injection molding, etc. In the manufacture of pharmaceutical tablets the method can also be used to control coating thickness in batch tablet coating operations, powder properties in wet granulation processes and powder moisture in batch drying. As can be seen, the advanced batch control method can be applied across many industries and can be implemented to increase control, decrease variability and improve process efficiency and process operability.

Bang-Bang Control

The method described above can be supplemented with bang-bang control. In one embodiment the advanced batch control method discussed herein is supplemented with bang-bang control. In another embodiment bang-bang control is applied without advanced batch control. In one embodiment the process variables are monitored and/or controlled via advanced batch control utilizing bang-bang control to achieve a desired set point or condition such as separation time.

It is often common for two or more batch or semi-batch processes to share equipment. Shared equipment refers to any equipment which can be shared by two or more batch processes. Shared equipment can include pumps, agitators, conveyors, slicers, product lines, heat exchangers, etc.

In one embodiment the method is performed on a system comprising at least two batch processing sets. A batch processing set refers to the equipment necessary to process a batch. A batch processing set can include kettles, pumps, agitators, heat exchangers, etc. In one embodiment a batch processing set consists only of the equipment that is dedicated to that batch. In one embodiment a first batch is being processed in a first batch processing set and a second batch is being processed in a second batch processing set. In one embodiment, at least one shared equipment is utilized by the first and second batch sets. In one embodiment, only one batch set may utilize the shared equipment at a time.

To maximize throughput and minimize downtime in one embodiment the batches that share equipment are spaced so that the equipment can be shared without any conflict. A conflict arises when two or more batches are calling for the shared equipment. In such a situation one of the batches must be stopped until the first batch is no longer requiring the shared equipment. Such a situation is undesirable as it decreases throughput, decreases efficiency, and can have a negative impact on product quality. If, for example, an exit conveyor is shared and a conflict arises then the product will be processed for greater than desired time. One skilled in the art will understand this can result in several disadvantages including the product being ruined from over or under cooking as well as increased product variability.

In one embodiment a first batch is initiated in a first batch processing set. Thereafter, a second batch is initiated in a second batch processing equipment. The batches can be initiated by any step that normally initiates a batch, including, for example, introducing material into the batch. At least one process variable for each of the first and second batches is monitored. Depending upon the results from monitoring the batches, at least one process variable on at least of the batches is adjusted using bang-bang control to prevent conflicts. In one embodiment, after the first batch has completed a third batch is initiated in the first batch processing set and the process is repeated. In one embodiment the system comprises more than two batches. In one such embodiment the system further comprises a third batch processing set which also shares equipment with the first and second batch processing sets. In one embodiment, more than one piece of equipment is shared by the various sets. In one embodiment the shared equipment is utilized by each batch at differing times. As an example, in one embodiment a first piece of shared equipment is utilized during initiation of each batch while a second piece of shared equipment is utilized during batch processing. In one embodiment comprising multiple pieces of shared equipment, the controller places greater priority on the second piece of shared equipment, as an example, than the first piece of shared equipment. For example, if the second piece of shared equipment is for removing the final product from the batch, this may take priority over initiating a new batch. In such circumstances, it may be more desirable to have a conflict with the first piece of shared equipment than with the second piece of shared equipment. Accordingly, different weights can be applied to different pieces of equipments to give one equipment more importance. The controller can utilize these weights in determining the appropriate adjustments.

For explanation purposes, a bang-bang control application will be discussed in reference to a kettle fryer. However, it should be noted that the invention is not so limited. The method described herein can be applied to virtually any batch or semi-batch operation which shares equipment.

FIG. 8 is a side profile view of a shared slicer and conveyor in one embodiment. FIG. 8 illustrates a main conveyor 801 and a slicer 802. The potatoes are sliced and stored in the slicer 802. In other embodiments a slicer 802 comprises a separate hopper which collects and stores the sliced potatoes. The main conveyor 801 conveys product received from the slicer 802 into the kettle fryer via the entrance conveyor 505 a, b. The entrance conveyor was described in reference to FIG. 5. FIG. 8 illustrates two entrance conveyors 505 a, b. These represent two kettle fryers. The bottom entrance conveyor 505 a is coupled to a first kettle fryer and the top entrance conveyor 505 b is coupled to a second kettle fryer. It should be noted that while the two entrance conveyors 505 a, b, are illustrated as being atop one another, in other embodiments they are adjacent to one another.

In one embodiment two or more kettle fryers share a common slicer 802 and main conveyor 801. This offers several benefits including reduced capital costs compared to having each kettle comprise its own slicer 802 and/or main conveyor 801. In operation the slicer 802 and main conveyor 801 work to introduce a first batch weight of potatoes into a first kettle. Thereafter the slicer 802 and main conveyor 801 transition to the second kettle and introduce a batch weight of potatoes. Thereafter the slicer 802 and conveyor 801 transition back to the first kettle and the process is repeated.

In one embodiment to avoid conflicts the batches are staggered so that they are out of phase. In one embodiment the batches are staggered so that they are out of phase relative to batch time. Batches are considered out of phase if the batches are equidistant apart in their total batch processing time. Thus, if a batch requires a total batch time of 10 minutes in one embodiment a second batch will begin after the first batch has been processed for 5 minutes. Total batch time is equal to the sum of the batch processing time and the recovery time. The batch processing time begins when the batch was initiated and is complete upon completion of the batch. The recovery time begins when the batch is complete and ends upon the initiation of a subsequent batch. Thus total batch time is the time between the initiation of successive batches. In one embodiment to ensure the batches are staggered as desired and to avoid conflicts, bang-bang control is utilized.

Bang-bang control is a method whereby a process variable is adjusted between at least two states to obtain a desired set point or process condition. A common example of a bang-bang controller is a thermostat. When a thermostat determines the temperature to be outside of the acceptable margin of the desired temperature the thermostat instructs the air conditioner to turn on. When the desired temperature has been reached the thermostat instructs the air conditioner to turn off. Thus, the air conditioner is instructed to operate between at least two defined states: on and off. The set point or process condition can be any set point, process condition, or process variable previously described. In one embodiment process condition is current processing time whereas in another embodiment the process condition is the total batch time or calculated total batch time. The calculated batch time can be calculated, estimated, or predicted with any method known in the art or discussed herein. In one embodiment an advanced batch control method is used to determine the total batch time.

In one embodiment at least one process variable on each of the batches is monitored. The process variables can be any process variable previously discussed including gas flow rate, temperature, processing time, separation time, calculated batch finish time, total batch time, etc.

In one embodiment comprising a kettle fryer, the process variable comprises gas flow rate. As previously described the kettles are heated to a specified temperature using gas. The temperature of the fryer can be increased by increasing the gas flow rate to the kettle heater.

FIG. 9 is a temperature and gas flow rate profile of two batches in one embodiment. The first batch temperature profile 901 is shown on the top of the graph and illustrates temperature of the first kettle as measured on the bottom of the kettle against time. The second batch temperature profile 903 shown in the middle of the graph illustrates temperature of the second kettle as measured on the bottom of the kettle against time. As the temperature profiles 901, 903 peak this illustrates the beginning of a new batch as a batch weight of potatoes is introduced into the kettle. In one embodiment a temperature of about 310° F. is reached before potatoes are introduced into the kettle. In one embodiment product discharge begins between about 298 to about 302° F. In one embodiment the goal is to keep the peaks of the two temperature profiles out of phase. In one embodiment the goal is to keep the peaks of the two temperature profiles separated by approximately half of the total batch time. Thus, as previously described, in one embodiment the goal is to start a second batch when the processing of the first batch is approximately half-way through the total batch time.

FIG. 9 also illustrates the first kettle gas flow rate profile 902 and the second kettle gas flow rate profile 904. As depicted the gas flow rate has three settings: a high fire flow rate 906, a low fire flow rate 905, and a low-low flow rate 907. In one embodiment a high fire flow rate 906 ranges from about 2,700 to about 4,000 scfh and represents the maximum possible flow gas flow rate. In another embodiment the high fire flow rate 906 ranges from about 2,800 to about 3,200 scfh. In one embodiment a low fire flow rate 905 ranges from about 500 to about 800 scfh. In another embodiment a low fire flow rate 905 ranges from about 600 to about 700 scfh. In one embodiment a low-low fire flow rate 907 ranges from about 5 to about 75 scfh and represents the minimum flow rate. In one embodiment the low-low fire flow rate 907 is only what is required to keep maintain the pilot light of the heater.

As can be seen after the batch is initiated the first gas flow rate 902 is increased from low fire 905 to high fire 906. The high fire gas flow rate 906 is maintained until it is determined that the desired temperature profile will be reached and the gas flow rate is reduced to low fire 905. This bang-bang control method is repeated throughout the process.

FIG. 9 illustrates a Monitor Point whereby the two or more batch processes are monitored. At this point the process variable and/or conditions are monitored to determine if action is necessary. As discussed a variety of variables can be monitored.

The Monitor Point can take place at a specified point, such as 5 minutes into processing or upon the happening of an event such as one or more batches reaching a certain temperature. In one embodiment the Monitor Point takes place at the same point in time for all batches whereas in another embodiment the Monitor Point does not take place at the same point in time for all batches. In one embodiment, for example, the Monitor Point for each batch occurs upon the batch reaching a specified temperature, regardless at which point in time the temperature is reached.

As depicted the controller at the Monitor Point considers the temperature profile of each batch, the processing time, and the predicted total batch time. The controller can consider a variety of other factors including process variables, set points, etc. The controller then determines if any action should be taken. As an example, if the controller at the Monitor Point determines that the batches are equally spaced within an acceptable margin then a control action may be unnecessary. In one embodiment the acceptable margin is within 20% of the desired condition. In one embodiment the acceptable margin is within 10% of the desired condition, while in still another embodiment the acceptable margin is within 5% of the desired condition. As an example if it is desirable that the batches achieve a separation time of about 5 minutes with a 20% margin then no adjustment is taken until the batches achieve a separation time of greater than about 4 minutes. Separation time refers to the difference in time between batch initiations in batches which share equipment. In one embodiment the separation time can be calculated, predicted, or estimated by taking the difference of the calculated total batch time of each batch. If it is predicted that the first batch will finish at 10:00 AM and the second batch will finish at 10:05 AM then a separation time of about 5 minutes has been achieved. The desired time separation will be dependent upon a variety of factors including the length of time a batch uses the shared equipment. In one embodiment comprising kettle fryers the total batch time ranges from about 9 minutes to about 11 minutes. In one embodiment the batch processing time ranges from about 9 minutes to about 11 minutes. In one embodiment the recovery time ranges from about 0 to about 2 minutes. As those skilled in the art will understand, in one embodiment it is desirable to minimize recovery time to increase efficiency and throughput. In one embodiment wherein the total batch time ranges from about 9 to 11 minutes the desired time separation is approximately equal to half of the total batch time. In one embodiment the desired time separation is about 20 to about 60% of the total batch processing time. In another embodiment comprising two batches the time separation is about 50% of the total batch time. In an embodiment comprising three batches the time separation between each batch is approximately ⅓ of the total batch time.

Any controller may be utilized in the monitoring and adjusting steps. In one embodiment an advanced batch controller is utilized whereas in another embodiment the PLC is the controller.

If at the Monitor Point the controller determines that the two batches are outside of the acceptable margin then a control action is taken. A control action can be adjusting any process variable previously discussed. Accordingly, gas flow rate, heating fluid flow rate, hold time, recovery time, processing time, recovery time, etc. can be adjusted. In one embodiment at least one process variable is adjusted to change the total batch time. In one embodiment at least one process variable is adjusted to achieve a desired separation time or calculated total batch time. In one embodiment at least one process variable is adjusted so that the total batch time is extended for at least one batch. In such an embodiment if the calculated total batch time was 10 minutes the adjusted calculated total batch time is 11 minutes.

As described above, in one embodiment the controller compares the calculated total batch time for one batch with the calculated total batch time for a second batch. The adjustment is calculated to yield the desired total batch time for each batch. In one embodiment the Control Action occurs only once per batch, while in other embodiments a batch will comprise two or more Control Actions.

In one embodiment the adjustments take place utilizing bang-bang control. Accordingly, in one embodiment the adjustments comprise varying at least one process variable between at least two states. The at least two states can comprise an on position and an off position, such as for a pump or an agitator. In such an operation bang-bang control would instruct when and how long the pump should operate. As an example, if a temperature was desired in a tank before discharge, bang-bang control can instruct a heating valve to operate from 0% open to 100% open to allow heating fluid to heat the tank as fast as possible. Once a desired temperature had been reached the controller using bang-bang control then instructs the heating valve to close. Additionally, the at least two states can comprise varying levels such as varying flow rates, varying RPMs, etc. The amount of time spent at each of said at least two states is determined by the controller. In one embodiment only two states are utilized whereas in other embodiments two or more states are utilized.

In one embodiment utilizing a kettle fryer, the gas flow rate is adjusted to control the batch finish time. As depicted in FIG. 9, the controller at the Monitor Point determined the monitored variables and/or conditions were not within the acceptable margin. Accordingly, a control action was initiated at the Control Action point. As depicted the first kettle was processing too fast compared to the second kettle. Put differently, the first and second kettle did not have the desired separation time. Accordingly, the first kettle would eventually catch the second kettle and create a conflict. In response, the controller decided to slow down the processing of the first kettle, and thus increase the total batch time, by adjusting at least one variable. In the embodiment depicted the gas flow rate was adjusted from the high fire gas flow rate 906 to a low-low fire gas flow rate 907. The time necessary for processing at the low-low fire gas flow rate 907 can be calculated using methods discussed herein. Holding for a determined time period at the low-low fire gas flow rate 907 has an effect on the temperature profile 901 of the first kettle. As can be seen at the point labeled Control Response the temperature profile temporarily levels for a period before subsequently increasing. This results in the slowing of the first batch so that it is out of phase with the second phase. Accordingly, a conflict is avoided. Further, as will be discussed below this increases the recovery time while not affecting the processing time. In one embodiment the process variable is adjusted until the desired separation time has been achieved within the acceptable margin.

In one embodiment the recovery time is adjusted while the processing time is left unaltered. As discussed herein, in some embodiments adjusting the processing time has an effect on the product and its final product qualities. In one embodiment adjusting the processing time has a negative impact on the final product. For example if the processing time is increased the product can be overcooked which can affect moisture content, oil content, etc. Likewise, if a product is undercooked then the desired moisture content may not be reached. Accordingly, in one embodiment the processing time is left unaltered and the recovery time is adjusted. In one embodiment the processing time has a variance of less than 10% across batches. In another embodiment the processing time has a variance of less than 5% across batches.

As previously discussed, in one embodiment the potatoes begin discharging at between about 298 to about 302° F. In one embodiment discharging takes about 50 seconds. Once the batch temperature has reached 310° F. potatoes are introduced into the batch. In one embodiment the potatoes are completely discharged as soon as the batch temperature reaches 310° F. so that potatoes are immediately introduced into the kettle. Such an embodiment has a recovery time of approximately zero. As can be seen in FIG. 9, the Control Action comprised decreasing the gas flow rate to the low-low gas flow rate 907 for a short period of time. The action took place prior to the discharge temperature was reached. Thereafter the flow rate was increased to a low gas flow rate 905 and the batch held until the peak temperature of about 310° F. was obtained. At that time additional potatoes were introduced into the batch. The time between when the potatoes were discharged and the time potatoes were introduced is the recovery time. Consequently, by reducing the gas flow rate the recovery time, and thus, the total batch time was increased which increased separation time. One benefit of adjusting the recovery time is that the processing time can remain uniform. Accordingly, in one embodiment the control action adjusts the recovery time.

In one embodiment a process variable for only one batch is adjusted. Put differently, in such an embodiment one batch is adjusted and the remaining batch or batches are not adjusted. In still other embodiments at least one process variable for one or more batches are adjusted.

While an embodiment has been described wherein a batch is slowed in other embodiments the processing rate of a batch is increased. Those skilled in the art will understand when to slow or speed a batch.

While only a single Monitor Point and Control Action point was illustrated other embodiments may comprise multiple Monitor and/or Control Points. For example, after making an adjustment the controller can utilize another Monitor Point to determine if further adjustments are necessary.

The above described method offers several benefits. One such benefit is the ability to decrease or eliminate conflicts. As discussed, this allows equipment to be successfully shared which results in decreased capital costs. Further, this results in increased throughput and less downtime.

Second, in one embodiment the above described method results in decreased product variability. As an example in reference to the kettle fried potato chips, processing time was often controlled by adjusting batch weight. Because it took a larger mass of potatoes a longer time to reach a desired temperature the total batch time could be increased by increasing batch weight. Likewise, total batch time could be decreased by using comparatively smaller batch weights. However, using inconsistent batch weights resulted in increased product variability. FIG. 10 is a graph showing the concentration of Acrylamide as a function of batch size in one embodiment. It can be seen that batch size has a significant correlation to Acrylamide. Thus, if batch size is increased in order to slow the batch processing time, the result could be increased Acrylamide formation.

Likewise, moisture content and oil content are also dependent upon batch size. Accordingly, often using different batch weights results in inconsistent product quality which is undesirable. In one embodiment the control method discussed herein results in decreased standard deviation for final product qualities and process variables. In one embodiment final product quality standard deviation was decreased by about 20 to about 40%.

In one embodiment, the method described herein allows the batch processing time to be controlled by adjusting the gas flow rate. Accordingly, the batch weight can be fixed, which decreases product variability. In one embodiment utilizing bang-bang control on a kettle fryer, the batch weight standard deviation was reduced by 86%. In one embodiment wherein bang-bang control was not utilized to control batch time, the batch weight had a standard deviation of 23.5 whereas with bang-bang control the standard deviation decreased to 3.5. Likewise the average moisture reduction standard deviation was reduced by 25%. In one embodiment the variance between successive batch weights was less than 10%. In another embodiment the variance between successive batch weights was less than 5%.

While the invention has been particularly shown and described with reference to a preferred embodiment, it will be understood by those skilled in the art that various changes in form and detail may be made therein without departing from the spirit and scope of the invention.

ADDITIONAL DESCRIPTION

The following clauses are offered as further description of the disclosed invention.

1. A batch control method in a system, said system comprising:

-   -   a first batch processing set;     -   a second batch processing set;     -   at least one shared equipment which is utilized by said first         and second batch processing set;     -   wherein said method comprises:     -   a. initiating a first batch in said first batch processing set;     -   b. initiating a second batch in said second batch processing         set;     -   c. monitoring at least one process variable on each of said         first and second batches;     -   d. adjusting at least one process variable on at least one of         said batches;         wherein said adjusting comprises utilizing bang-bang control,         and wherein said adjusting step prevents conflicts.         2. The method according to any preceding clause wherein said         first batch processing set comprises a frying kettle.         3. The method according to any preceding clause wherein said         process variable of step c) comprises temperature.         4. The method according to any preceding clause wherein said         process variable of step c) comprises processing time.         5. The method according to any preceding clause wherein said         process variable of step c) comprises separation time.         6. The method according to any preceding clause wherein said         process variable of step c) comprises calculated total batch         time.         7. The method according to clause 6 wherein said adjusting of         step d) comprises adjusting the total batch time of at least one         batch.         8. The method according to clause 6 wherein said adjusting of         step d) comprises adjusting the total batch time of at least one         batch, wherein the processing time of the batch is not adjusted.         9. The method according to clause 6 wherein said adjusting of         step d) comprises adjusting the recovery time.         10. The method according to any preceding clause wherein said         adjusting of step d) comprises extending the total batch time of         at least one batch.         11. The method according to any preceding clause wherein said         process variable of step d) comprises separation time.         12. The method according to any preceding clause wherein said         adjusting comprises adjusting at least one process variable to         achieve a desired separation time.         13. The method according to clause 12 wherein said desired         separation time is about half of the batch processing time.         14. The method according to any preceding clause wherein said         process variable of step d) comprises gas flow rate.         15. The method according to any preceding clause wherein said         adjusting of step d) comprises decreasing a gas flow rate.         16. The method according to any preceding clause wherein said         initiating of step b) comprises staggering said initiating so         that said second batch is out of phase with said first batch.         17. The method according to any preceding clause wherein said         adjusting step consists of adjusting at least one process         variable on only one of said batches.         18. The method according to any preceding clause wherein said         adjusting step comprises adjusting at least one process variable         on both said first and second batches.         19. The method according to any preceding clause wherein said         system further comprises a third batch processing set and said         method further comprises step e) of initiating a third batch in         said third batch processing set.         20. The method according to any preceding clause wherein said         adjusting of step d) comprises utilizing bang-bang control, and         wherein said bang-bang control comprises adjusting between two         states.         21. The method according to clause 20 wherein said two states         comprise an off state and an on state.         22. The method according to any preceding clause wherein said         adjusting of step d) comprises utilizing bang-bang control, and         wherein said bang-bang control comprises adjusting between more         than two states.         23. A batch control method in for a kettle fryer system, said         system comprising:     -   a first kettle fryer;     -   a second kettle fryer;     -   at least one shared equipment which is utilized by said first         and second kettle fryers;     -   wherein said method comprises:     -   a. initiating a first batch in said first kettle fryer;     -   b. initiating a second batch in said second kettle fryer;     -   c. monitoring at least one process variable on each of said         first and second batches;     -   d. adjusting at least one process variable on at least one of         said batches;         wherein said adjusting comprises utilizing bang-bang control,         and wherein said adjusting step prevents conflicts.         24. The method according to clause 23 wherein said adjusting of         step d) comprises increasing total batch time for at least one         batch.         25. The method according to clause 24 wherein said increasing         total batch time does not comprise increasing batch processing         time.         26. The method according to clause 23 wherein said adjusting of         step d) comprises increasing recovery time for at least one         batch.         27. The method according to clause 23 wherein said initiating of         step a) comprises introducing a batch weight of potatoes into         said kettle fryer.         28. The method according to clause 23 further comprising:     -   e. initiating a third batch in said first kettle fryer.         29. The method according to clause 28 wherein said adjusting of         step d) comprises adjusting at least one process variable, and         wherein said adjusting results in the delaying said initiating         of step e).         30. The method according to clause 28 wherein said initiating of         step e) and initiating of step a) comprise introducing a batch         weight of potatoes into said first kettle fryer, wherein the         variance between said batch weight of said first batch and said         batch weight of said third batch is less than 5%.         31. The method according to clause 23 wherein said shared         equipment comprises a slicer.         32. The method according to any preceding clause wherein said         process variable of step c) comprises temperature.         33. The method according to any preceding clause wherein said         process variable of step c) comprises separation time.         34. The method according to any preceding clause wherein said         process variable of step d) comprises gas flow rate. 

1. A batch control method in a system, said system comprising: a first batch processing set; a second batch processing set; at least one shared equipment which is utilized by said first and second batch processing set; wherein said method comprises: a. initiating a first batch in said first batch processing set; b. initiating a second batch in said second batch processing set; c. monitoring at least one process variable on each of said first and second batches; d. adjusting at least one process variable on at least one of said batches; wherein said adjusting comprises utilizing bang-bang control, and wherein said adjusting step prevents conflicts.
 2. The method of claim 1 wherein said first batch processing set comprises a frying kettle.
 3. The method of claim 1 wherein said process variable of step c) comprises temperature.
 4. The method of claim 1 wherein said process variable of step c) comprises processing time.
 5. The method of claim 1 wherein said process variable of step c) comprises separation time.
 6. The method of claim 1 wherein said process variable of step c) comprises calculated total batch time.
 7. The method of claim 6 wherein said adjusting of step d) comprises adjusting the total batch time of at least one batch.
 8. The method of claim 6 wherein said adjusting of step d) comprises adjusting the total batch time of at least one batch, wherein the processing time of the batch is not adjusted.
 9. The method of claim 6 wherein said adjusting of step d) comprises adjusting the recovery time.
 10. The method of claim 1 wherein said adjusting of step d) comprises extending the total batch time of at least one batch.
 11. The method of claim 1 wherein said process variable of step d) comprises separation time.
 12. The method of claim 1 wherein said adjusting comprises adjusting at least one process variable to achieve a desired separation time.
 13. The method of claim 12 wherein said desired separation time is about half of the batch processing time.
 14. The method of claim 1 wherein said process variable of step d) comprises gas flow rate.
 15. The method of claim 1 wherein said adjusting of step d) comprises decreasing a gas flow rate.
 16. The method of claim 1 wherein said initiating of step b) comprises staggering said initiating so that said second batch is out of phase with said first batch.
 17. The method of claim 1 wherein said adjusting step consists of adjusting at least one process variable on only one of said batches.
 18. The method of claim 1 wherein said adjusting step comprises adjusting at least one process variable on both said first and second batches.
 19. The method of claim 1 wherein said system further comprises a third batch processing set and said method further comprises step e) of initiating a third batch in said third batch processing set.
 20. The method of claim 1 wherein said adjusting of step d) comprises utilizing bang-bang control, and wherein said bang-bang control comprises adjusting between two states.
 21. The method of claim 20 wherein said two states comprise an off state and an on state.
 22. The method of claim 1 wherein said adjusting of step d) comprises utilizing bang-bang control, and wherein said bang-bang control comprises adjusting between more than two states.
 23. A batch control method in for a kettle fryer system, said system comprising: a first kettle fryer; a second kettle fryer; at least one shared equipment which is utilized by said first and second kettle fryers; wherein said method comprises: a. initiating a first batch in said first kettle fryer; b. initiating a second batch in said second kettle fryer; c. monitoring at least one process variable on each of said first and second batches; d. adjusting at least one process variable on at least one of said batches; wherein said adjusting comprises utilizing bang-bang control, and wherein said adjusting step prevents conflicts.
 24. The method of claim 23 wherein said adjusting of step d) comprises increasing total batch time for at least one batch.
 25. The method of claim 24 wherein said increasing total batch time does not comprise increasing batch processing time.
 26. The method of claim 23 wherein said adjusting of step d) comprises increasing recovery time for at least one batch.
 27. The method of claim 23 wherein said initiating of step a) comprises introducing a batch weight of potatoes into said kettle fryer.
 28. The method of claim 23 further comprising: e. initiating a third batch in said first kettle fryer.
 29. The method of claim 28 wherein said adjusting of step d) comprises adjusting at least one process variable, and wherein said adjusting results in the delaying said initiating of step e).
 30. The method of claim 28 wherein said initiating of step e) and initiating of step a) comprise introducing a batch weight of potatoes into said first kettle fryer, wherein the variance between said batch weight of said first batch and said batch weight of said third batch is less than 5%.
 31. The method of claim 23 wherein said shared equipment comprises a slicer.
 32. The method of claim 1 wherein said process variable of step c) comprises temperature.
 33. The method of claim 1 wherein said process variable of step c) comprises separation time.
 34. The method of claim 1 wherein said process variable of step d) comprises gas flow rate. 